CN108435239A - A kind of catalyst and the preparation method and application thereof of coproduction alkene and aromatic hydrocarbons - Google Patents
A kind of catalyst and the preparation method and application thereof of coproduction alkene and aromatic hydrocarbons Download PDFInfo
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- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
- B01J29/48—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing arsenic, antimony, bismuth, vanadium, niobium tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
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- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
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- B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
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- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
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- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
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- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
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- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
- B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
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Abstract
The invention belongs to CO, CO2Catalytic conversion technique field, more particularly to a kind of catalyst and the preparation method and application thereof of coproduction alkene and aromatic hydrocarbons, the catalyst is by being constituted with fischer-tropsch activity component part and with aromatization activity component part, wherein fischer-tropsch activity component part is made of fischer-tropsch activity component, adjuvant component and inert material clad, aromatization activity component part is by zeolite molecular sieve and inert material clad, or zeolite molecular sieve, auxiliary agent and inert material clad are constituted, and CO is fastened in the caltalyst2Or CO or both mixtures can be under suitable reaction condition, alkene (C2 C5) content is up to 70% in gas phase hydrocarbon products, and for aromatic hydrocarbons total content up to 95% or more, wherein paraxylene content is up to 50%, can be from CO the present invention provides one in liquid hydrocarbon2, CO add the variation route of hydrogen coproduction alkene and aromatic hydrocarbons.
Description
Technical field
The invention belongs to CO, CO2The catalyst of catalytic conversion technique field more particularly to a kind of coproduction alkene and aromatic hydrocarbons and
Preparation method and application.
Background technology
Low-carbon alkene includes ethylene, propylene and butylene and aromatic hydrocarbons include benzene, toluene and dimethylbenzene (BTX) is important
Industrial chemicals, be mainly derived from the cracking of naphtha.With the reduction of crude resources and becoming increasingly conspicuous for environmental problem, together
When shale gas scale exploitation so that obtain alkene from petroleum path and aromatic hydrocarbons be challenged, also become unsustainable.Cause
This, Non oil-based route preparing low-carbon olefins and aromatic hydrocarbons are increasingly taken seriously.
Using synthesis gas, the direct producing light olefins of carbon dioxide or aromatic hydrocarbons as a substitute technology route, for utilizing
China compared with horn of plenty coal resources, alleviate dependence to petroleum resources, be of great significance.Currently reported synthesis gas
Or the technical process of carbon dioxide aromatic hydrocarbons directly processed will be mainly by that will have the function of synthesis gas transformation function and dehydroaromatizationof
Two kinds of catalyst be first placed on series connection double bed reactor or be placed in single reactor in a manner of being mixed between particle or in particle
Middle realization.For example, domestic the used two reactor of Shanxi coalification is respectively provided with two types catalyst, synthesis gas can be passed through
Dimethyl ether conversion is aromatic hydrocarbons.And Guan Naijia seminars of Nankai University report by F- T synthesis (FTS) catalyst Fe/MnO with
Ga/HZSM-5 catalyst physicals mix, and arenes selectivity is close to 50% at 1.1MPa, 270 DEG C.
However when directly using mixed catalyst, since molecular sieve catalyst easily inactivates, it is not easy the expense from high activity
It is separated in time in fischer-tropsch catalyst.Also, when the content of molecular sieve is more than a certain amount of, it can also seriously affect fischer-tropsch catalysts
Activity.In addition, the optimum operation condition of fischer-tropsch reaction and aromatization does not often match well.These problems will all have
The application of synthesis gas or carbon dioxide conversion for aromatic hydrocarbons may be limited.Further, in current report, low-carbon alkene in gas phase
It is obtained while cannot be highly selective simultaneously with aromatic hydrocarbons in liquid phase.
Invention content
In order to solve the above technical problems, the object of the present invention is to provide the catalyst and its system of a kind of coproduction alkene and aromatic hydrocarbons
Preparation Method can realize CO or CO with application, the catalyst2Or both one step of mixture add hydrogen coproduction alkene and virtue with high selectivity
Hydrocarbon, the catalyst have very high gas phase selectivity of light olefin and liquid phase arenes selectivity simultaneously after above-mentioned raw materials reaction,
Paraxylene especially in light aromatics is expected to industrially apply.Simultaneously effective avoid fischer-tropsch activity component and virtue
It influences each other between structure active component.
The present invention proposes a kind of catalyst of coproduction alkene and aromatic hydrocarbons, can be to CO2Or CO or both hydrogenation mixtures connection
It includes fischer-tropsch activity component part and aromatization activity component part, fischer-tropsch activity composition portion to produce alkene and aromatic hydrocarbons, the catalyst
It includes fischer-tropsch activity component and inert material clad to divide, and aromatization activity component part includes zeolite molecular sieve.
Further, fischer-tropsch activity component part and aromatization activity component part mixed in the form of particle or powder and
At the weight ratio of the two is 0.05-20.
Further, in aromatization activity component part further include inert material clad.
Further, further include auxiliary agent in fischer-tropsch activity component part and/or aromatization activity component part.
Further, fischer-tropsch activity component includes with one or more of Fe, Co, Ru, Cu, Zn, Zr, Cr element
The loaded or non-loaded catalyst that oxide is constituted.
Further, auxiliary agent includes one in P, V, Cr, Mn, Na, K, Cu, Zn, Ga, Ge, Zr, Mo, S, Pd, Ag, W, Re, Co
Kind or two or more oxides.
Further, the inert material in inert material clad includes any one in silica, aluminium oxide or two
Kind.
Further, zeolite molecular sieve includes any one or more in ZSM-5, MCM-22, MCM-49.
Further, the auxiliary agent weight percent in fischer-tropsch activity component part and aromatization activity component part respectively
For 0.1-30% (in terms of oxide).
Further, inert material clad is respectively in fischer-tropsch activity component part and aromatization activity component part
Weight percent is 0.1-40%.
Further, the silica alumina ratio in zeolite molecular sieve is：Si/Al=10-500.
Further, when fischer-tropsch activity group is divided into loaded catalyst in fischer-tropsch activity component part, carrier includes
SiO2、Al2O3、TiO2, SiC, any one or more in activated carbon, vehicle weight accounts for the 50- of fischer-tropsch activity composition weight
99%.
The present invention proposes the preparation method of above-mentioned fischer-tropsch activity component part, includes the following steps：It will be with or without
There is the fischer-tropsch activity component of auxiliary agent to be impregnated in the solution of organic compound of the presoma containing inert material, stirring, roasts drying
It arrives.
Further, the fischer-tropsch activity component of auxiliary agent is contained or not contain using isometric or excess solution impregnation or coprecipitated
It is prepared by shallow lake method.
Further, mixing time 0-24h.
Further, revolving removes solvent and in 30-250 DEG C of dry 0-24h after stirring.
Further, calcination temperature is 250-700 DEG C, roasting time 0.5-24h.
The present invention proposes the preparation method of above-mentioned aromatization activity component part, includes the following steps：It will be with or without
There is the zeolite molecular sieve of auxiliary agent to be impregnated in the solution of organic compound of the presoma containing inert material, stirring, roasts drying
It arrives.
Further, mixing time 0-24h.
Further, revolving removes solvent and in 30-250 DEG C of dry 0-24h after stirring.
Further, calcination temperature is 250-700 DEG C, roasting time 0.5-24h.
Further, the zeolite molecular sieve preparation method containing auxiliary agent is as follows：Using equi-volume impregnating or ion exchange
Zeolite molecular sieve is impregnated into the soluble-salt containing metallic element by method or excessive infusion process, and dry later, roasting obtains.
Further, soluble-salt includes nitrate, carbonate, acetate, sulfate, molybdate, tungstates and chloride
In any one or more.
Further, drying steps include that revolving removes solvent then in 30-250 DEG C of dry 0-24h.
Further, calcination temperature is 250-700 DEG C, roasting time 0.5-24h.
The present invention proposes above-mentioned catalyst in CO or CO2Or both mixture direct hydrogenation coproduction alkene and aromatic hydrocarbons chemical combination
Application in the reaction of object.
Further, the reaction condition that catalyst of the invention is applied is：CO or CO2Or both mixture and H2Body
Product ratio is 0.1-10.
Further, CO and CO in reaction raw materials2Volume ratio be 0-100.
Further, reaction temperature is 150~600 DEG C.
Further, reaction pressure is 0.1~5MPa.
Further, reaction velocity is 500~50000h-1。
Further, the reaction time is 1~5000h.
The present invention proposes above-mentioned catalyst using the preceding method for carrying out pre-reduction treatment, the pretreatment used also Primordial Qi
Atmosphere includes any one or more in hydrogen, carbon monoxide, methane, ethane, ethylene gas.
Further, pretreatment temperature is 150~600 DEG C.
Further, Pretreatment pressures are 0.1~3Mpa.
Further, pretreatment gas volume space velocity is 1000~50000h-1。
Further, pretreatment time be 1~for 24 hours.
According to the above aspect of the present invention, the present invention has at least the following advantages：
(1) technique is not necessarily to as indirect method technique from synthesis gas through methanol or dimethyl ether, then prepares alkene or aromatic hydrocarbons,
Technological process is simplified, operating cost is low, greatly reduces investment.
(2) catalyst prepared is suitable for coal base, biomass-based and natural gas base synthesis gas and contains CO2For original
Material coproduction prepares the reaction process of alkene and aromatic hydrocarbons.
(3) have fischer-tropsch activity and aromatization activity part after having coated inert material in the catalyst prepared by,
It is inactivated due to preventing two kinds of alternate influence each other of activity, while avoiding low-carbon alkene from being hydrogenated to form alkane so that product
In with the paraxylene in very high gas phase selectivity of light olefin and liquid phase arenes selectivity, especially light aromatics, have
Prestige is industrially applied.
Specific implementation mode
Embodiment of the present invention is described in detail below in conjunction with embodiment, but those skilled in the art will
Understand, the following example is merely to illustrate the present invention, and should not be taken as limiting the scope of the invention.
The person that is not specified actual conditions in embodiment, carries out according to conventional conditions or manufacturer's recommended conditions.Agents useful for same
Or production firm person is not specified in instrument, being can be with conventional products that are commercially available.
One, CO or CO2Or both hydrogenation mixture coproduction alkene and arenes catalytic agent preparation
Embodiment 1
The first step takes a certain amount of ferric nitrate, manganese nitrate to be dissolved in deionized water, using ammonium hydroxide as precipitating reagent in pH=
It is precipitated under the conditions of 8.0, through aging, is filtered, washed and is dried 12 hours at 120 DEG C, iron is finally roasted 5 hours to obtain at 500 DEG C
Manganese atom is than the sedimentation type FeMn catalyst for 95 to 5.It is 1 that the catalyst prepared, which is impregnated in mass ratio,:0.8:1:0.5
Ethyl orthosilicate, CTAB, second alcohol and water solution in, and be stirred continuously 12 hours, revolving removal solvent and done later at 120 DEG C
It roasts 5 hours, is obtained with SiO at dry 12 hours, 500 DEG C2The component part with fischer-tropsch activity of coating, through analyzing SiO2
Coating accounts for the 6.5% of the moiety by weight.
Second step takes silica alumina ratio to be impregnated in above-mentioned identical teos solution for 15 HZSM-5 molecular sieves, and
It is stirred continuously 12 hours, the solvent of revolving removal later is 12 hours dry at 120 DEG C, and roast at 500 DEG C 5 hours and obtained have
The component part of aromatization activity, through analyzing SiO2Coating accounts for the 7.4% of the moiety by weight.
Third walks, to sample made from the first step and second step carry out respectively tabletting, broken, screening 20-40 mesh particle with
Mass ratio is 1：2 mode carries out particle mixing, and the catalyst A that can be used for reacting is made.
Embodiment 2
The first step takes a certain amount of ferric nitrate, is precipitated under the conditions of pH=8.0 as precipitating reagent using ammonium hydroxide, through aging,
It is filtered, washed and 12 hours dry at 120 DEG C, sedimentation type Fe catalyst is finally roasted 5 hours to obtain at 500 DEG C；It uses later
Equi-volume process prepares the FeK catalyst of K loads, and the wherein mass fraction of K is 0.8%；Then the FeK catalyst is impregnated in matter
Amount is than being 1:0.8:1:0.5 ethyl orthosilicate, CTAB, second alcohol and water solution in, and be stirred continuously 12 hours, rotate later
Removal solvent simultaneously roasts 5 hours at 120 DEG C at drying 12 hours, 500 DEG C, obtains with SiO2Coating with fischer-tropsch activity
Component part, through analyzing SiO2Coating accounts for the 7.2% of the moiety by weight.
Second step uses equi-volume impregnating that silica alumina ratio is impregnated in the nitric acid of certain content for 15 HZSM-5 molecular sieves
In cobalt liquor, the solvent of revolving removal later is 12 hours dry at 120 DEG C, and 5 hours obtained Co/HZSM-5 are roasted at 500 DEG C
Catalyst, the wherein mass fraction of Co are 5wt%；Sample obtained is then impregnated in above-mentioned identical teos solution
In, and be stirred continuously 12 hours, the solvent of revolving removal later is 12 hours dry at 120 DEG C, and roasts 5 hours and make at 500 DEG C
The component part with aromatization activity is obtained, through analyzing wherein SiO2Coating accounts for the 6.9% of the moiety by weight.
Third walks, to sample made from the first step and second step carry out respectively tabletting, broken, screening 20-40 mesh particle with
Mass ratio is 1：2 mode carries out particle mixing, and the catalyst B that can be used for reacting is made.
Embodiment 3
SiC is impregnated into the aqueous solution of ferric nitrate and sodium nitrate, Zhi Houxuan by the first step using isometric dipping method
It boils off and is dried 12 hours at 120 DEG C except solvent, and roast 5 hours obtained NaFe/SiC loaded catalysts at 500 DEG C, wherein
The load capacity of Fe is 30%, and the load capacity of sodium is 1.8%；Then the NaFe/SiC loaded catalysts are impregnated in mass ratio is
1:0.8:1:0.5 ethyl orthosilicate, CTAB, second alcohol and water solution in, and be stirred continuously 12 hours, revolving removal later is molten
Agent simultaneously roasts 5 hours at 120 DEG C at drying 12 hours, 500 DEG C, obtains with SiO2The composition portion with fischer-tropsch activity of coating
Point, through analyzing SiO2Coating accounts for the 5.8% of the moiety by weight.
Second step uses equi-volume impregnating that silica alumina ratio is impregnated in the nitric acid of certain content for 15 HZSM-5 molecular sieves
In Gallium solution, the solvent of revolving removal later is 12 hours dry at 120 DEG C, and 5 hours obtained Ga/HZSM-5 are roasted at 500 DEG C
Catalyst, the wherein mass fraction of Ga are 6wt%；Sample obtained is then impregnated in above-mentioned identical teos solution
In, and be stirred continuously 12 hours, the solvent of revolving removal later is 12 hours dry at 120 DEG C, and roasts 5 hours and make at 500 DEG C
The component part with aromatization activity is obtained, through analyzing wherein SiO2Coating accounts for the 5.5% of the moiety by weight.
Third walks, to sample made from the first step and second step carry out respectively tabletting, broken, screening 20-40 mesh particle with
Mass ratio is 1：2 mode carries out particle mixing, and the catalyst C that can be used for reacting is made.
Embodiment 4
Component part (the SiO with fischer-tropsch activity in Example 22The FeK catalyst of coating cladding) and embodiment 3
In the component part (SiO with aromatization activity2The Ga/HZSM-5 catalyst of coating cladding), tabletting is carried out respectively, is broken
Broken, screening 20-40 mesh particle is with mass ratio for 1：5 mode carries out particle mixing, and the catalyst D that can be used for reacting is made.
Embodiment 5
Component part (the SiO with fischer-tropsch activity in Example 22The FeK catalyst of coating cladding) and embodiment 3
In the component part (SiO with aromatization activity2The Ga/HZSM-5 catalyst of coating cladding), tabletting is carried out respectively, is broken
Broken, screening 20-40 mesh particle is with mass ratio for 1：10 mode carries out particle mixing, and the catalyst E that can be used for reacting is made.
Two, application of institute's invention catalyst in coproduction alkene and aromatic hydrocarbons
The fixed component part quality with fischer-tropsch activity is 1g, catalyst is placed in the reactor continuously flowed, instead
Procatalyst is answered to be all made of in hydrogen, carbon monoxide, methane, ethane, ethylene gas one or more kinds of gas prereduction one
It fixes time, is then cooled to reaction temperature and introduces reaction gas progress successive reaction.Reaction gas has 3 kinds：(1) 30vol%CO2、
65vol%H2And 5vol%N2；(2) 45%CO, 45%H2And 10%N2.Wherein N2As interior standard gas, for calculating CO or CO2's
Conversion ratio.Product normal pressure on-line analysis after cold-trap is furnished with the gas phase of conductance cell and hydrogen ion flame detector by one simultaneously
Chromatography is analyzed, chromatographic condition be 5A molecular sieve packed columns andCapillary packed column (50 meters), temperature programming (initial temperature
It 50 DEG C, is kept for 10 minutes, subsequent 5 DEG C/min is warming up to 200 DEG C, is kept for 10 minutes)；In cold-trap product by another equipped with hydrogen from
The gas-chromatography off-line analysis of sub- flame detector, chromatographic condition are HP-1 capillarys packed column (50 meters), temperature programming (initial temperature 50
DEG C, kept for 5 minutes, subsequent 5 DEG C/min is warming up to 250 DEG C, is kept for 10 minutes).
Embodiment 6
Catalyst A-E is respectively placed in fixed bed reactor, in H2400 DEG C are warming up to 5 DEG C/min in atmosphere,
Under normal pressure, air speed 1000h-1Restore 10h.Then cooling introduces reaction gas (1) and is reacted, reaction pressure 1.0MPa, reaction
Air speed 5000h-1, 340 DEG C, successive reaction 30h of reaction temperature, average CO2Conversion ratio and each selectivity of product or distribution results are shown in
Table 1.Wherein A, D, E catalyst have investigated the component part with fischer-tropsch activity and the composition portion mass ratio with aromatization activity
Influence.
Catalytic performance of 1 different catalysts of table (A-E) to reaction raw materials (1)
As can be seen from the table, for CO2Hydrogenation reaction for, the overall selectivity of gaseous hydrocarbon and liquid hydrocarbon is reachable
Nearly 90%, olefin(e) centent is up to 70% or more in gaseous hydrocarbon, and up to 95%, wherein paraxylene contains aromatic hydrocarbons total content in liquid hydrocarbon
Amount is up to 50%.Particularly, for catalyst D, E, when with fischer-tropsch activity component part and with the group of aromatization activity
At part mass than up to 1：5 and 1：When 10, higher CO is still maintained2Conversion ratio, at this point, arenes selectivity is substantially in product
Degree increases.
Embodiment 7
Catalyst A~E is respectively placed in fixed bed reactor, in H2In atmosphere 400 are warming up to 5 DEG C/min
DEG C, under normal pressure, air speed 1000h-1Restore 10h.Then cooling introduces reaction gas (2) and is reacted, reaction pressure 1.0MPa, instead
Answer air speed 5000h-1, 340 DEG C, successive reaction 30h of reaction temperature, average conversion and each selectivity of product or distribution results are shown in Table
2.Wherein A, D, E catalyst have investigated the component part with fischer-tropsch activity and the composition portion mass ratio with aromatization activity
It influences.
Catalytic performance of 2 different catalysts of table (A-E) to reaction raw materials (2)
Embodiment 8
Catalyst B is placed in fixed bed reactor, in H2400 DEG C are warming up to 5 DEG C/min in atmosphere, normal pressure
Under, air speed 1000h-1Restore 10h.Then cooling introduces reaction gas (1) and is reacted, reaction pressure 1.0MPa, reaction velocity
5000h-1, 260 DEG C, 300 DEG C, 340 DEG C and 380 DEG C of reaction temperature, successive reaction 30h investigates the influence of reaction temperature.CO2It is flat
Equal conversion ratio and each selectivity of product the results are shown in Table 3.
Catalytic performances of the 3 catalyst B of table to reaction raw materials (1) at a temperature of differential responses
Embodiment 9
Catalyst B is placed in fixed bed reactor, in H2400 DEG C are warming up to 5 DEG C/min in atmosphere, normal pressure
Under, air speed 1000h-1Restore 10h.Then cooling introduces reaction gas (1) and is reacted, reaction velocity 5000h-1, reaction temperature
340 DEG C, reaction pressure 0.5MPa, 1.0MPa, 2.0MPa and 3.0MPa, successive reaction 30h investigate the influence of reaction pressure.CO2
Average conversion and each selectivity of product the results are shown in Table 4.
Catalytic performances of the 4 catalyst B of table to reaction raw materials (1) under differential responses pressure
Comparative example 1
Without SiO in Example 12FeMn active components of cladding and without SiO2The HZSM-5 molecular sieves of cladding are direct
Tabletting, broken, screening 20-40 mesh particle are with mass ratio for 1：2 mode carries out particle mixing, and the catalysis that can be used for reacting is made
Agent F.The catalyst F for being 1.0 grams by FeMn constituent mass is placed in fixed bed reactor, in H2With 5 DEG C/min in atmosphere
400 DEG C, under normal pressure are warming up to, air speed 1000h-1Restore 10h.Then cooling introduces reaction gas (1) and is reacted, reaction pressure
1.0MPa, reaction velocity 5000h-1, 340 DEG C, successive reaction 30h of reaction temperature, average CO2Conversion ratio and each selectivity of product or
Distribution results are shown in Table 5.
Comparative example 2
Without SiO in Example 22FeK active components of cladding and without SiO2The Co/HZSM-5 components of cladding are direct
Tabletting, broken, screening 20-40 mesh particle are with mass ratio for 1：2、1：5 and 1：10 mode carries out particle mixing, is made and can be used for
Catalyst G, H and I of reaction.The catalyst for being 1.0 grams by FeK constituent mass is placed in fixed bed reactor, in H2Atmosphere
400 DEG C, under normal pressure are warming up to 5 DEG C/min in enclosing, air speed 1000h-1Restore 10h.Then cooling introduces reaction gas (1) and carries out
Reaction, reaction pressure 1.0MPa, reaction velocity 5000h-1, 340 DEG C, successive reaction 30h of reaction temperature, average CO2Conversion ratio and
Each selectivity of product or distribution results are shown in Table 5.
Catalytic performance of 5 different catalysts of table (F-I) to reaction raw materials (1)
As can be seen from Table 5, catalyst does not have SiO2When cladding, gaseous hydrocarbon product is mainly based on saturated alkane, together
When aromatic hydrocarbons in paraxylene content it is very low.Particularly, for catalyst H, I, when with fischer-tropsch activity component part and
Composition portion mass ratio with aromatization activity is up to 1：5 and 1：When 10, CO2Conversion ratio drastically declines.
Although the present invention has been described by way of example and in terms of the preferred embodiments, it is not limited to the present invention, any to be familiar with this skill
The people of art can do various change and modification, therefore the protection model of the present invention without departing from the spirit and scope of the present invention
Enclosing be subject to what claims were defined.
Claims (10)
1. a kind of catalyst of coproduction alkene and aromatic hydrocarbons, it is characterised in that：Including fischer-tropsch activity component part and aromatization activity
Component part, fischer-tropsch activity component part include fischer-tropsch activity component and inert material clad, aromatization activity component part
Including zeolite molecular sieve.
2. the catalyst of coproduction alkene and aromatic hydrocarbons according to claim 1, it is characterised in that：Aromatization activity component part
In further include inert material clad.
3. the catalyst of coproduction alkene and aromatic hydrocarbons according to claim 1 or 2, it is characterised in that：Fischer-tropsch activity composition portion
Point and/or aromatization activity component part in further include auxiliary agent.
4. the catalyst of coproduction alkene and aromatic hydrocarbons according to claim 3, it is characterised in that：Auxiliary agent is being taken in terms of oxide
Weight percent in the active component part of support and aromatization activity component part is respectively 0.1-30%.
5. the catalyst of coproduction alkene and aromatic hydrocarbons according to claim 1, it is characterised in that：Fischer-tropsch activity component part and
Aromatization activity component part is mixed in the form of particle or powder, and the weight ratio of the two is 0.05-20.
6. the catalyst of coproduction alkene and aromatic hydrocarbons according to claim 1, it is characterised in that：Fischer-tropsch activity component include with
The loaded or non-loaded catalyst that one or more of Fe, Co, Ru, Cu, Zn, Zr, Cr element oxide is constituted.
7. the catalyst of coproduction alkene and aromatic hydrocarbons according to claim 1, it is characterised in that：In inert material clad
Inert material includes any one or two kinds in silica, aluminium oxide.
8. the catalyst of coproduction alkene and aromatic hydrocarbons according to claim 1, it is characterised in that：Inert material clad is distinguished
Weight percent in fischer-tropsch activity component part and aromatization activity component part is 0.1-40%.
9. a kind of preparation method of fischer-tropsch activity component part, it is characterised in that：The fischer-tropsch activity component part is wanted for right
The fischer-tropsch activity component part in 1-8 any one of them catalyst, preparation method is asked to include the following steps：It will be with or without
There is the fischer-tropsch activity component of auxiliary agent to be impregnated in the solution of organic compound of the presoma containing inert material, stirring, roasts drying
It arrives.
10. the catalyst of claim 1-8 any one of them coproduction alkene and aromatic hydrocarbons is in CO or CO2Or both mixture it is direct
Add the application in the reaction of hydrogen coproduction alkene and aromatic compound.
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| CN109569704A (en) * | 2018-12-25 | 2019-04-05 | 江南大学 | A kind of catalyst directly preparing alkene and aromatic hydrocarbons for synthesis gas and its application |
| CN109942359A (en) * | 2019-03-16 | 2019-06-28 | 复旦大学 | Composite Double bed catalyst and its with the method for hydrogenation of carbon dioxide aromatic hydrocarbons |
| CN112844390A (en) * | 2021-02-03 | 2021-05-28 | 江南大学 | Iron-nickel bimetallic Fischer-Tropsch catalyst for preparing low-carbon olefin, preparation method and application |
| CN112871200A (en) * | 2021-02-03 | 2021-06-01 | 江南大学 | Catalyst system for preparing light aromatic hydrocarbon from synthesis gas and application thereof |
| CN114471744A (en) * | 2020-11-13 | 2022-05-13 | 中国科学院大连化学物理研究所 | Pretreatment method and application of iron-based catalyst |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109569704A (en) * | 2018-12-25 | 2019-04-05 | 江南大学 | A kind of catalyst directly preparing alkene and aromatic hydrocarbons for synthesis gas and its application |
| CN109942359A (en) * | 2019-03-16 | 2019-06-28 | 复旦大学 | Composite Double bed catalyst and its with the method for hydrogenation of carbon dioxide aromatic hydrocarbons |
| CN114471744A (en) * | 2020-11-13 | 2022-05-13 | 中国科学院大连化学物理研究所 | Pretreatment method and application of iron-based catalyst |
| CN114471744B (en) * | 2020-11-13 | 2023-09-19 | 珠海市福沺能源科技有限公司 | Pretreatment method of iron-based catalyst and application thereof |
| CN112844390A (en) * | 2021-02-03 | 2021-05-28 | 江南大学 | Iron-nickel bimetallic Fischer-Tropsch catalyst for preparing low-carbon olefin, preparation method and application |
| CN112871200A (en) * | 2021-02-03 | 2021-06-01 | 江南大学 | Catalyst system for preparing light aromatic hydrocarbon from synthesis gas and application thereof |
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